Classifications

• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01D—SEPARATION
  • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01D—SEPARATION
  • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
  • B01D61/02—Reverse osmosis; Hyperfiltration ; Nanofiltration
  • B01D61/04—Feed pretreatment
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01D—SEPARATION
  • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
  • B01D61/36—Pervaporation; Membrane distillation; Liquid permeation
  • B01D61/364—Membrane distillation
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01D—SEPARATION
  • B01D69/00—Semi-permeable membranes for separation processes or apparatus characterised by their form, structure or properties; Manufacturing processes specially adapted therefor
  • B01D69/02—Semi-permeable membranes for separation processes or apparatus characterised by their form, structure or properties; Manufacturing processes specially adapted therefor characterised by their properties
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01D—SEPARATION
  • B01D2325/00—Details relating to properties of membranes
  • B01D2325/02—Details relating to pores or porosity of the membranes

Definitions

• the present invention relates to the concentration of liquids by osmotic distillation and to hydrophobic porous barriers or membranes suitable therefor.
• Membrane distillation is a process for the evaporation and subsequent condensation of volatiles from a solution via a membrane.
• an hydrophobic (non-wettable) membrane such as polyvinylidine difluoride (PVDF), polytetrafluoro ethylene (teflon) or polypropylene.
• PVDF polyvinylidine difluoride
• teflon polytetrafluoro ethylene
• polypropylene The driving force of membrane distillation is the vapour pressure gradient resulting from the temperature difference between the two solutions (i.e., between the two surfaces of the membrane).
• Water evaporates at the solution-membrane interface on the higher temperature side of the membrane and is transported across the membrane to the cooler side thereof.
• the water vapour pressure is either condensed or discarded on reaching the cool side of the membrane. Heat must be continually supplied to the evaporating surface to provide the latent heat of vaporisation. The converse applies at the condensing surface.
• N vapour flux (g.mol/m 2 /s)
• r membrane pore radius (m)
• ⁇ membrane porosity (o)
• R universal gas constant (J/mol/K)
• T average temperature (K)
• M vapour molecular weight (kg/g.mol)
• ⁇ P trans-membrane pressure drop (Pa)
• l membrane pore length (m).
• the vapour flux across the membrane is inversely proportional to the membrane thickness and thus the use of thinner membranes is beneficial.
• the heat exchanging properties and therefore the effective temperature gradients across the membrane vary with thickness.
• There are two types of heat flow through the membrane which have to be taken into consideration, namely:- (i) Q C being the heat flow (Kjoule/m 2 /sec) associated with evaporation of the solvent from one side of the membrane and condensation on the other; and
• the membrane characteristic Cp is again a function of the membrane geometry. Again the efficiency is independent of thickness of the membrane for a given wall temperature difference. In both cases the vapour flux N is therefore dependent of a given membrane material and structure, only of T 2 w - T 1 w) these values being related to T 1 and T 2 by
• membrane distillation is a process where a trade off is necessary when choosing the membrane thickness between the non-acceptable heat losses associated with thin membranes and the non-acceptable low flux associated with the low membrane coefficient of thick membranes. Disclosure of the Invention
• an hydrophobic semipermeable barrier for the concentration of a solution by a process of osmotic distillation, said barrier characterised in that it comprises a semipermeable matrix of a high thermal conductibility material, having a thickness of less than 50 microns (preferably less than 20 microns and more preferably less than 10 microns), a minimum porosity of 50% of the surface area of the barrier, and pore dimensions such that the flux is proportional to the pore radius (Knudsen) or to the square of the pore radius (Poiseuille).
• a system adapted to perform the concentration of a dilute solution of low osmotic pressure by a process of osmotic distillation, which process utilises an hydrophobic semipermeable diffusion barrier of the type described herein having as its driving force the difference in osmotic pressure between two fluids interfacing said barrier to achieve the concentration of the fluid having the lower osmotic pressure.
• an osmotic distillation process for the concentration of a first fluid by bringing said fluid into contact with one side of a semipermeable barrier of the type described herein whilst simultaneously bringing a second fluid into contact with the opposite side of the membrane, said second fluid having a higher osmotic pressure than said first fluid whereby solvent from said first fluid is transferred across the semipermeable barrier in the vapour state under the influence of an osmotic pressure gradient to the second fluid resulting in the concentration of the first fluid.
• Membrane distillation is a process for the evaporation and subsequent condensation of volatiles from a solution.
• the evaporating and condensing surfaces remain in close proximity, being separated by a microporous membrane.
• the segregation of the two liquid surfaces requires that only vapours and gases be transmitted through the pores of the membrane.
• the driving force for vapour transport across the membrane is the temperature difference between the two sides of the membrane.
• Osmotic distillation the process or system of the present invention, is different to membrane distillation.
• the driving force for osmotic distillation is the difference in vapour pressure associated with the difference in osmotic pressure between the liquids on opposite sides of the membrane.
• Fig. 1 is a graphical representation of the Knudsen diffusion and Poiseuille flow regimes.
• Fig. 2 and Fig. 3 represent temperature profiles for membrane distillation and osmotic distillation processes, respectively.
• the driving force for osmotic distillation is the difference in vapour pressure associated with the difference in osmotic pressure ⁇ 2 - ⁇ 1 as expressed in the equation
• the higher the osmostic pressure inside the liquid the lower the partial pressure at the surface of the liquid.
• the temperature on the evaporation side of the membrane is lower than the temperature on the condensation side.
• the temperature profiles are reversed. Because the temperature profiles are reversed, and because the membrane acts as a heat exchanger, the transfer of heat is in the opposite direction to that in membrane distallation.
• osmotic distillation where there is a temperature gradient present across the membrane, the temperature gradient is supplemented by an osmotic pressure gradient in the opposite direction. This is brought about by contacting the membrane on the cool side by a solution of high solute concentration relative to that on the hot side. The osmotic pressure of the concentrated solution acts to lower the vapour pressure above it and hence the vapour pressure gradient resulting from the temperature difference is enhanced.
• the driving force for osmotic distillation can be a very small temperature difference when compared to membrane distillation. In osmotic distillation temperature differences of only a few degrees are common whereas in membrane distillation it is not unusual to have a difference of temperature of the order of 50oC. Thus the driving force in osmotic distillation might only be, say, about 2% of the driving force in membrane distillation.
• the flux is proportional to the membrane pore radius.
• the flux is proportional to the radius squared - i.e., if you double the radius the flux is increased by a factor of four.
• Membranes for osmotic distillation are manufactured by any process which will provide a relatively open pore structure, including processes common to the textile industry, such as weaving, knitting, the Docan (spunbound) process, plasma reticulation, and the like.
• Non-woven processes can also be used e.g. the dry non-woven process and the wet non-woven process of the paper industry.
• Pore dimensions can be as large as practicable, compatible with the requirement that only vapour and not liquid is permitted to pass through the pores. Pore dimension of fractions of a millimetre (e.g. 0.5mm) are envisaged.
• the membranes are made of highly conductive fibres, such as stainless steel or copper, to facilitate heat transfer.
• the fabric of the barrier or membrane will be as thin as possible e.g. of the order of about 10 microns. Further, the fabric of the barrier should be totally hydrophobic.
• the wire is immersed in teflon to coat the wire prior to weaving.
• the membrane or barrier also has a lateral permeabiltiy to gases e.g. to the atmosphere.
• the osmotic distillation barriers of the present invention have extremely high flux and have potential applications in many areas e.g. concentration of fruit juices, milk and coffee, and recovery of potable water from seawater.
• concentration of fruit juices, milk and coffee e.g., aqueous saline, aqueous saline, aqueous saline, aqueous saline, aqueous saline, s, and coffee, and recovery of potable water from seawater.
• the following is a summary of the general characteristics for Osmotic Distillation.
• Porosity For Knudsen and Poiseuille flow membrane the flux will be proportional to the membrane porosity. A minimum porosity of 50% is required but a sufficient amount of material for heat transfer is needed also. The porosity of osmotic distillation membranes can be lower than the porosity of membranes used in membrane' distillation. Thickness: The thinnest possible membrane are required. Pore dimensions:
• Flux is proportional to pore radius (Knudsen) or square of the pore radius (Poiseuille). Ideally, the largest possible pores compatible with membrane strength and Schmerber height (the water pressure entry express in height of water) is required. Hydrophobicity:
• the membrane material is chosen from reticulated fluoro or chloro fluorinated polymers, saturated stereospecific polyofines or any polymer with the lowest possible moisture regain and the highest possible angle of contact with water.

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• Engineering & Computer Science (AREA)
• Water Supply & Treatment (AREA)
• Chemical & Material Sciences (AREA)
• Chemical Kinetics & Catalysis (AREA)
• Nanotechnology (AREA)
• Separation Using Semi-Permeable Membranes (AREA)
• Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
• Physical Or Chemical Processes And Apparatus (AREA)
• External Artificial Organs (AREA)

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• 1987
  • 1987-05-05 BR BR8707689A patent/BR8707689A/pt not_active IP Right Cessation
  • 1987-05-05 US US07/283,274 patent/US5098566A/en not_active Expired - Fee Related
  • 1987-05-05 DE DE8787903213T patent/DE3783910D1/de not_active Expired - Lifetime
  • 1987-05-05 WO PCT/AU1987/000132 patent/WO1987006850A1/en not_active Ceased
  • 1987-05-05 AT AT87903213T patent/ATE84985T1/de not_active IP Right Cessation
  • 1987-05-05 EP EP87903213A patent/EP0304426B1/en not_active Expired - Lifetime
  • 1987-05-05 KR KR1019880700002A patent/KR950007918B1/ko not_active Expired - Lifetime
  • 1987-05-05 AU AU73982/87A patent/AU607142B2/en not_active Ceased
  • 1987-05-05 JP JP62503048A patent/JPH01503282A/ja active Pending
• 1988
  • 1988-01-04 DK DK000988A patent/DK988A/da not_active Application Discontinuation

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